Hot solids process having an output suitable for the input to a petrochemical process

ABSTRACT

A hot solids process wherein a predetermined output, which is designed to be suitable for use as an input to a petrochemical process, is capable of being generated through the use of the hot solids process. The mode of operation of such a hot solids process is designed to be such that preferably a portion of the otherwise normally unusable product output, which is produced from a petrochemical process, is designed to be utilized as an input to the hot solids process for purposes of generating from the hot solids process the predetermined output that is suitable for use as an input to a petrochemical process.

CROSS-REFERENCE TO RELATED APPLICATIONS

The present invention claims the benefit of co-pending U.S. ProvisionalPatent Application Ser. No. 61/165,042, entitled “HOT SOLIDS PROCESSSELECTIVELY OPERABLE FOR COMBUSTION PURPOSES AND GASIFICATION PURPOSES”,and co-pending U.S. Provisional Patent Application 61/165,069, entitled“HOT SOLIDS PROCESS SELECTIVELY OPERABLE BASED ON THE TYPE OFAPPLICATION THAT IS INVOLVED”, and co-pending U.S. Provisional PatentApplication 61/165,094, entitled “HOT SOLIDS PROCESS SELECTIVELYOPERABLE BASED ON WHAT THE SPECIFIC NATURE OF THE HOT SOLIDS PROCESS'PRIMARY PURPOSE IS” all of which are incorporated herein by reference intheir entirety.

TECHNICAL FIELD

This invention relates generally to a hot solids process that is capableof generating a predetermined output that is designed to be suitable foruse as an input to a petrochemical process. Moreover, the presentinvention relates to such a hot solids process that is designed toemploy a portion of the otherwise normally unusable product output,which is produced from such a petrochemical process, for purposes ofgenerating, in accordance with the present invention, the output fromthe hot solids process that is designed to be suitable for use as aninput to said petrochemical process.

BACKGROUND

The World today faces a critical challenge as all nations strive tosatisfy basic human requirements—food, shelter, clothing and work—thatare so dependent on adequate supplies of energy. The great increase inthe use of energy has been met mostly by fossil fuels—primarily, coal,oil and gas. The belief is that environmental concerns, security ofsupply, and economic impacts must all be balanced as the demand forenergy continues to increase. Real economic growth and energy usenevertheless still remain inextricably linked.

While the quest for ultimate solutions to provide adequate energysupplies continues, near term, interim solutions must be considered formeeting the immediate growth in demand for energy. Technologicalimprovements in the mining, drilling, moving, processing, and using offossil fuels can, of course, stretch energy resource reserves, as can adetermined effort at conservation of energy. Similarly, the utilizationof advanced clean fossil fuel technologies involving the employment ofvarious forms of hot solids processes such as, by way of exemplificationand not limitation, fossil fuel gasification, fluidized-bed combustion,or hybrid combustion-gasification fossil fuel technologies, are capableof having the effect of that of widening the use of the World's vastfossil fuel resources.

In accordance with the mode of operation of electrical power generationsystems, as is well known to most, the steam that is produced by steamgenerators, which are employed in such electrical power generationsystems, from the combustion of fossil fuel therein is designed to beemployed in steam turbines. Such steam, which commonly is both at a hightemperature and at a high pressure, is expanded in the aforementionedsteam turbine in order to thereby effect a rotation of the steamturbine. Such rotation of the steam turbine in turn is operative in aknown manner to cause a generator that is suitably operatively connectedto the steam turbine to rotate as well. Then, when the generatorundergoes such rotation, a conductor is made to move through a magneticfield thereby causing an electric current to be generated. Theaforedescribed mode of operation is fundamentally the basis upon whichelectrical power generation systems continue to be predicated even tothis day.

In an effort to realize higher efficiencies for electrical powergeneration systems, attempts have been known to have been made toincrease the temperatures and the pressures at which the steamgenerators that are employed in such electrical power generation systemsare capable of being operated. Such efforts to date have resulted insteam generators being supplied commercially for employment inelectrical power generation systems that are capable of being operatedat subcritical pressure conditions or that are capable of being operatedat supercritical pressure conditions. Improvements in the strength ofthe materials from which such steam generators, which are intended foremployment in electrical power generation systems, are designed to beconstructed have permitted such materials, and thus such steamgenerators, to be operated both at such higher temperatures and at suchhigher pressures.

Discussing further the advanced clean fossil fuel technologies to whichreference has been had above previously wherein various forms of hotsolids processes are employed, and in particular to that of fossil fuelgasification technologies, attention is first directed in thisconnection, by way of exemplification and not limitation, to U.S. Pat.No. 2,602,809, which issued on Jul. 8, 1952 to The M. W. KelloggCompany. The teachings of U.S. Pat. No. 2,602,809 are considered to berepresentative of an exemplification of an early development in thecontinuing development of fossil fuel gasification technologies of thetype wherein hot solids processes are employed. To this end, inaccordance with the teachings thereof, the teachings of U.S. Pat. No.2,602,809 are directed to a proves, which is said to be particularlysuited for the gasification of low-grade solid carbon-containingmaterials. More specifically, insofar as the mode of operation of theprocess to which the teachings of U.S. Pat. No. 2,602,809 are directedis concerned, the solid carbon-containing materials are designed to beoxidized in order to convert such solid carbon-containing materials tocarbon oxides by virtue of the indirect oxidation thereof with air insuch a manner that the nitrogen of the air does not contaminate theproduct gas. Such gasification of the solid carbon-containing materialsis accomplished by virtue of the alternate oxidation and reduction of afluidized metal oxide. According to the teachings of U.S. Pat. No.2,602,809, solid fuels are subjected to being converted to gases as aconsequence of the contacting by a metal oxide with finely-divided solidcarbon-containing materials under conditions such as to cause the metaloxide to be reduced and the carbon of the solid fuel to be oxidized tocarbon oxides, with the metal oxide being the principal source of oxygenthat is required for the oxidation of the carbon. Then, after the metaloxide has been reduced, the reduced metal oxide is subjected to beingre-oxidized whereupon the process cycle is capable of being repeatedonce again.

With further regard to the fossil fuel gasification technologies of theadvanced clean fossil fuel technologies to which reference has been hadabove previously wherein various forms of hot solids processes areemployed, attention is next directed herein, by way of exemplificationand not limitation, to U.S. Pat. No. 4,602,573, which issued on Jul. 29,1986 to Combustion Engineering, Inc. The teachings of U.S. Pat. No.4,602,573 are considered to be representative of an exemplification of afurther development in the continuing evolution of fossil fuelgasification technologies of the type wherein hot solids processes areemployed. To this end, in accordance with the teachings thereof, theteachings of U.S. Pat. No. 4,602,573 are stated to be directed to amethod of gasifying and combusting a carbonaceous fuel and, moreparticularly to an integrated process wherein a sulfur andnitrogen-bearing carbonaceous fuel is gasified to produce a carbonmonoxide-rich low BTU fuel gas that is deigned to be subsequentlycombusted with additional carbonaceous fuel in a steam generator. Morespecifically, insofar as the mode of operation of the process to whichthe teachings of U.S. Pat. No. 4,602,573 are directed is concerned, afirst portion of sulfur and nitrogen-bearing carbonaceous fuel isgasified in a gasification reactor in a reducing atmosphere of air toproduce a hot, char-containing, carbon monoxide-rich fuel gas having alow BTU content. Thereafter, a sulfur capturing material is introducedinto the gasification reactor so that the gasifying of the carbonaceousfuel is carried out in the presence of the sulfur capturing materialwhereby a substantial portion of the sulfur in the carbonaceous fuelbeing gasified is captured by the sulfur capturing material.

Attention will next be directed herein further to the advanced cleanfossil fuel technologies to which reference has been had abovepreviously wherein various forms of hot solids processes are employedand in particular to that of fluidized-bed combustion technologies.Thus, more specifically, attention is therefore directed in thisconnection, by way of exemplification and not limitation, to U.S. Pat.No. 4,111,158, which issued on Sep. 5, 1978 to MetallgesellschaftAktiengesellschaft. The teachings of U.S. Pat. No. 4,111,158 areconsidered to be representative of an exemplification of an earlydevelopment in the continuing development of the fluidized-bedcombustion technologies of the type wherein hot solids processes areemployed. To this end, in accordance with the teachings thereof, theteachings of U.S. Pat. No. 4,111,158 are stated to be directed to amethod of and an apparatus for carrying out an exothermic process inwhich a solid feed contains a combustible such as, for example,carbonaceous or sulfurous compounds. Continuing, insofar as the mode ofoperation of the method of and the apparatus for to which the teachingsof U.S. Pat. No. 4,111,158 are directed is concerned, the combustiblecompounds of the solid feed are designed to be burned underapproximately stoichiometric conditions in a fluidized bed. Thereafter,the solids, which are produced as a consequence of such burning of thecombustible compounds of the solid feed and which are withdrawn from thefluidized bed are caused to be recycled back to the fluidized bed, whilethe heat that is produced from such burning of the combustible compoundsof the solid feed is available to be recovered.

Regarding further the fluidized-bed combustion technologies of theadvanced clean fossil fuel technologies to which reference has been hadabove previously wherein various forms of hot solids processes areemployed, attention is next directed herein, by way of exemplificationand not limitation, to U.S. Pat. No. 5,533,471, which issued on Jul. 9,1996 to A. Ahlstrom Corporation. The teachings of U.S. Pat. No.5,533,471 are considered to be representative of an exemplification of afurther development in the continuing evolution of fluidized-bedcombustion technologies of the type wherein hot solids processes areemployed. To this end, in accordance with the teachings thereof, theteachings of U.S. Pat. No. 5,533,471 are stated to be directed to asystem and to a method that allow the temperature of the fluidized bedreactor to be controlled efficiently, allowing adequate heat transfersurface area for cooling of solid materials. More specifically, insofaras the mode of operation of the system and of the method to which theteachings of U.S. Pat. No. 5,533,471 are directed is concerned, acirculating (fast) fluidized bed and a bubbling (slow) fluidized bed areutilized. Continuing, these two (2) fluidized beds are mounted adjacenteach other with first and second interconnections between them,typically with the fluidizing gas introducing grid of the bubblingfluidized bed being below that of the circulating fluidized bed. Becausethe bubbling fluidized bed has a substantially constant densitythroughout, with a clear demarcation line at the top thereof, the firstinterconnection is provided above the top of the bubbling fluidized bedso that the pressure and density conditions between the two (2)fluidized beds result in a flow of particles from the circulatingfluidized bed to the bubbling fluidized bed through the firstinterconnection. However, since the average density in the bubblingfluidized bed is higher than the density in the circulating fluidizedbed, the pressure and density conditions cause the particles aftertreatment in the bubbling fluidized bed (e.g., after the cooling of theparticles therein) to return to the circulating fluidized bed throughthe second interconnection.

Discussing further the advanced clean fossil fuel technologies to whichreference has been had above previously wherein various forms of hotsolids processes are employed, and in particular that of hybridcombustion-gasification technologies, attention is first directed inthis connection, by way of exemplification and not limitation, to U.S.Pat. No. 4,272,399, which issued on Jun. 8, 1981 to the MonsantoCompany. The teachings of U.S. Pat. No. 4,272,399 are considered to berepresentative of an exemplification of an early development in thecontinuing evolution of the hybrid combustion-gasification technologiesof the type wherein hot solids processes are employed. To this end, inaccordance with the teachings thereof, the teachings of U.S. Pat. No.4,272,399 are stated to be directed to a unified process for producinghigh purity synthesis gas from carbon-containing materials. Morespecifically, insofar as the mode of operation of the unified process towhich the teachings of U.S. Pat. No. 4,272,399 are directed isconcerned, a metal-oxygen containing material, which can becharacterized as a heat and oxygen carrier and which can be referred togenerally as an oxidant, is used as the transfer agent of oxygen andheat for oxidatively gasifying carbon-containing material. Continuing,steam, carbon dioxide, synthesis gas or mixtures thereof are employed tofluidize and transport the oxidant through an up-flow, co-currentsystem. Thus, in accordance with the mode of operation of the subjectunified process, synthesis gas is first oxidized and heated by theoxidant to form water and carbon dioxide in an oxidant reducing zoneprior to contact of the oxidant and gases with the carbon-containingmaterial in a gasifying zone. In addition, the carbon-containingmaterials are oxidized to predominately carbon monoxide and hydrogen ina manner such that the nitrogen contained in the air does notcontaminate the product synthesis gas. Furthermore, the gasification ofthe carbon-containing material is accomplished by the alternateoxidation and reduction of a fluidized oxidant. Then, after suchgasification, the reduced oxidant, which may be in the form of theelemental metal or lower oxidized state is re-oxidized in an oxidizingzone and the cycle is then repeated.

Regarding further the hybrid combustion-gasification technologies of theadvanced clean fossil fuel technologies to which reference has been hadabove previously wherein various forms of hot solids processes areemployed, attention is next directed herein, by way of exemplificationand not limitation, to U.S. Pat. No. 7,083,658, which issued on Aug. 1,2006 to ALSTOM Technology Ltd., which is incorporated herein byreference. The teachings of U.S. Pat. No. 7,083,658 are considered to berepresentative of an exemplification of a further development in thecontinuing evolution of hybrid combustion-gasification technologies ofthe type wherein hot solids processes are employed. To this end, inaccordance with the teachings thereof, the teachings of U.S. Pat. No.7,083,658 are stated to be directed to apparatus utilizing fossil fuels,biomass, petroleum coke, or any other carbon bearing fuel to producehydrogen for power generation, which minimizes or eliminates the releaseof carbon dioxide (CO2). More specifically, insofar as the mode ofoperation of the apparatus to which the teachings of U.S. Pat. No.7,083,658 are directed is concerned, a gasifier is provided forproducing a gas product from a carbonaceous fuel, which comprises afirst chemical process loop including an exothermic oxidizer reactor andan endothermic reducer reactor. Continuing, the exothermic oxidizerreactor has a CaS inlet, a hot air inlet and a CaSO4/waste gas outlet.Whereas, the endothermic reducer reactor has a CaSO4 inlet in fluidcommunication with the exothermic oxidizer reactor CaSO4/waste gasoutlet, a CaS/gas product outlet in fluid communication with theexothermic oxidizer reactor CaS inlet, and a materials inlet forreceiving the carbonaceous fuel. Moreover, CaS is oxidized in air in theexothermic oxidizer reactor to form hot CaSO4, which is discharged tothe endothermic reducer reactor. Furthermore, hot CaSO4 and carbonaceousfuel that is received in the endothermic reducer reactor undergo anendothermic reaction utilizing the heat content of the CaSO4 with thecarbonaceous fuel stripping the oxygen from the CaSO4 to form CaS andthe gas product. Thereafter, the CaS is discharged to the exothermicoxidizer reactor, and with the gas product being discharged from thefirst chemical process loop.

It is, therefore, an object of the present invention to provide a hotsolids process.

It is also an object of the present invention to provide such a hotsolids process that is capable of generating an output.

It is another object of the present invention to provide such a hotsolids process that is capable of generating such an output that isdesigned to be suitable for use as an input to a petrochemical process.

It is still another object of the present invention to provide such ahot solids process that is designed to employ a portion of the otherwisenormally unusable product output, which is produced from such apetrochemical process, for purposes of generating in accordance with thepresent invention the output from the hot solids process of the presentinvention that is designed to be suitable for use as an input to such apetrochemical process.

Yet another object of the present invention is to provide such a hotsolids process that is relatively inexpensive to provide, is relativelyuncomplicated to employ, and is characterized by its great versatilityinsofar as the applicability thereof to petrochemical processes isconcerned.

SUMMARY OF THE INVENTION

In accordance with the present invention a hot solids process isprovided, which is capable of generating a predetermined output that isdesigned to be suitable for use as an input to a petrochemical process.To this end, the mode of operation, in accordance with the presentinvention of such a hot solids process, is such that preferably aportion of the otherwise normally unusable product output, which isproduced from such a petrochemical process, is designed to be employedas an input to the hot solids process of the present invention forpurposes of generating in accordance with the present invention thepredetermined output from the hot solids process of the presentinvention, which is designed to be suitable for use as an input to saidpetrochemical process.

Continuing, in accordance with the present invention the mode ofoperation of the hot solids process of the present invention is suchthat preferably a limestone based sorbent, such as, by way ofexemplification and not limitation, CaS, is designed to be combusted inan oxidizing reactor, such oxidizing reactor preferably, by way ofexemplification and not limitation, being a circulating bed reactor,which is designed to be selected from a group of reactors that includesa fixed bed reactor, a bubbling bed reactor, a circulating bed reactor,a transport reactor, and an entrained bed reactor, in order to therebyproduce hot CaSO4 from the combustion of such limestone based sorbent.This hot CaSO4 is then in turn designed to be employed in a reducingreactor, such reducing reactor preferably, by way of exemplification andnot limitation, being a circulating bed reactor, which is designed to beselected from a group of reactors that includes a fixed bed reactor, abubbling bed reactor, a circulating bed reactor, a transport reactor,and an entrained bed reactor, for purposes of generating thepredetermined output, which is designed to be suitable for use as aninput to a petrochemical process.

With further regard to the mode of operation of the hot solids processof the present invention, the inputs to the oxidizing reactor, which isemployed in accordance with the mode of operation of the hot solidsprocess of the present invention, when the fuel that is designed to becombusted in accordance therewith comprises a carbonaceous fuel, suchas, preferably a portion of the otherwise normally unusable productoutput, which is produced from a petrochemical process, and wherein aportion of such otherwise normally unusable product output, which isproduced from a petrochemical process, and which more particularlycomprises petcoke and/or oil residuals that are known to be otherwiseproduced as normally unusable product outputs from a petrochemicalprocess, and when the predetermined output that is being generated inaccordance with the preferred mode of operation of the hot solidsprocess of the present invention is designed to be suitable for use asan input to a petrochemical process, include CaS and air, and theoutputs from such an oxidizing reactor in such a case include ash,CaSO4, and N2. Whereas, the inputs to the reducing reactor, which isemployed in accordance with the mode of operation of the hot solidsprocess of the present invention, when the fuel that is designed to becombusted in accordance therewith comprises a carbonaceous fuel, suchas, preferably a portion of the otherwise normally unusable productoutput, which is produced from a petrochemical process, and wherein aportion of such otherwise normally unusable product output, which isproduced from a petrochemical process, and which more particularlycomprises petcoke and/or oil residuals that are known to be otherwiseproduced as normally unusable product outputs from a petrochemicalprocess, and when the predetermined output that is being generated inaccordance with the preferred mode of operation of the hot solidsprocess of the present invention is designed to be suitable for use asan input to a petrochemical process, include the carbonaceous fuel,CaCO3, steam, and CaSO4, and the output from such a reducing reactor insuch a case is designed to be the predetermined output, which is beinggenerated in accordance with the preferred mode of operation of the hotsolids process of the present invention such that the predeterminedoutput generated from the hot solids process of the present invention issuitable for use as an input to a petrochemical process.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 of the drawing is a schematic diagram of a preferred embodimentof the mode of operation of a hot solids process that functions inaccordance with the present invention to generate a predeterminedoutput, which is suitable for use as an input to a petrochemicalprocess, the latter petrochemical process also being schematicallydepicted as well in FIG. 1.

DETAILED DESCRIPTION

Referring now to FIG. 1 of the drawing, there is depicted therein aschematic diagram of a hot solids process, generally denoted by thereference numeral 10 in FIG. 1 of the drawing, that is designed to beoperable in accordance with the present invention for purposes ofgenerating a predetermined output, such as, by way of exemplificationand not limitation, H2 or syngas and steam, and with the latterpredetermined output being denoted by the arrow 12 in FIG. 1 of thedrawing. The predetermined output 12 from the hot solids process 10 isdesigned in accordance with the present invention to be suitable for useas an input to a petrochemical process, the latter petrochemical processbeing denoted generally by the reference numeral 14 in FIG. 1 of thedrawing. To this end, the mode of operation, in accordance with thepresent invention of the hot solids process 10, is such that preferablya portion of the otherwise normally unusable product output, denoted bythe reference numeral 16 in FIG. 1 of the drawing, which is producedfrom the petrochemical process 14, is designed to be utilized as aninput to the hot solids process 10 of the present invention for purposesof generating in accordance with the present invention the predeterminedoutput 12 from the hot solids process 10 of the present invention thatis designed to be suitable for use as an input to the petrochemicalprocess, which is schematically depicted at 14 in FIG. 1 of the drawing.The remainder, which is denoted by the reference numeral 17 in FIG. 1 ofthe drawing, of the otherwise normally unusable product output 16 thatis produced from the petrochemical process 14, which is schematicallydepicted in FIG. 1 of the drawing, is designed so as to be capable ofbeing discharged from the petrochemical process 14 in any conventionalmanner, which is deemed to be suitable for use for such a purpose.

Continuing, the hot solids process of the present invention inaccordance with the preferred mode of operation thereof is designed toutilize air; a carbonaceous fuel, such as, by way of exemplification andnot limitation, the portion of the otherwise normally unusable productoutput, which is 16 from a petrochemical process, such as, thepetrochemical process that is schematically depicted at 14 in FIG. 1 ofthe drawing, and wherein such a portion of the otherwise normallyunusable product output 16, which is produced from the petrochemicalprocess 14, and which preferably comprises petcoke and/or oil residualsthat are known to be producible as an otherwise normally unusableproduct output from a petrochemical process, such as, the petrochemicalprocess 14 that is schematically depicted in FIG. 1 of the drawing; asource of calcium (e.g., calcium oxide); and steam to effect therewiththe generation of the predetermined output 12, which is designed to besuitable for use as an input to a petrochemical process, such as, thepetrochemical process that is schematically depicted at 14 in FIG. 1 ofthe drawing.

With further reference to FIG. 1 of the drawing, a reducing reactor,denoted generally by the reference numeral 18 in FIG. 1 of the drawing,selected from a group of reactors that includes a fixed bed reactor, abubbling bed reactor, a circulating bed reactor, a transport reactor andan entrained bed reactor and preferably comprising a circulating bedreactor, and an oxidizing reactor, denoted generally by the referencenumeral 20 in FIG. 1 of the drawing, selected from a group of reactorsthat includes a fixed bed reactor, a bubbling bed reactor, a circulatingbed reactor, a transport reactor and an entrained bed reactor andpreferably comprising a circulating bed reactor, are each designed to beemployed in the hot solids process 10 of the present invention, inaccordance with the preferred mode of operation thereof. Continuing, inaccordance with the preferred embodiment of the hot solids process 10 ofthe present invention, the carbonaceous fuel, such as, by way ofexemplification and not limitation, the portion of the otherwisenormally unusable product output 16 that is produced from thepetrochemical process, which is schematically depicted at 14 in FIG. 1of the drawing, that is designed to be supplied from the petrochemicalprocess 14 as an input to the reducing reactor 18, is designed to beburned in the reducing reactor 18 preferably using air indirectly. Tothis end, a source of calcium (i.e., calcium oxide), and with the lattersource of calcium being denoted by the arrow 22 in FIG. 1 of thedrawing, which is designed to be added, in accordance with the preferredmode of operation of the hot solids process 10 of the present invention,is also supplied, by way of exemplification and not limitation, as aninput to the reducing reactor 18. However, such source of calcium 22could equally well be supplied elsewhere in the hot solids process 10 ofthe present invention other than as an input to the reducing reactor 18,without departing from the essence of the present invention. Such sourceof calcium 22, which may be selected from the group including oflimestone (CaCO3) or lime (CaO) or gypsum or the spent bed material froma circulating bed boiler, by way of exemplification and not limitation,preferably comprises limestone (CaCO3). With further reference thereto,such limestone (CaCO3) 22, which is added in accordance with thepreferred mode of operation of the hot solids process 10 of the presentinvention, is designed to be operative to capture in the reducingreactor 18 the sulfur (S), which is contained in the carbonaceous fuel16, such as to thereby produce calcium sulfide (CaS) therefrom in thereducing reactor 18.

Continuing, such calcium sulfide (CaS), as denoted by the arrow 24 inFIG. 1 of the drawing, is then made to exit from the reducing reactor 18as an output therefrom, whereupon such calcium sulfide (CaS) 24 isdesigned to be supplied as an input to the oxidizing reactor 20. In theoxidizing reactor 20, this calcium sulfide (CaS) 24 is designed to beburned in a heat liberation reaction with air, and with the latter airbeing denoted by the arrow 26 in FIG. 1 of the drawing, which isdesigned to be supplied as an input to the oxidizing reactor 20, such asto thereby effect the production therefrom of calcium sulfate (CaSO4) inthe oxidizing reactor 20. This calcium sulfate (CaSO4), as is denoted bythe arrow 28 in FIG. 1 of the drawing, is then designed to be made toexit as an output from the oxidizing reactor 20, whereupon this calciumsulfate (CaSO4) 28 is designed to be cycled to the reducing reactor 18as an input thereto for purposes of thereby producing therefrom thesupply of oxygen and of heat that is required both in order to burn thecarbonaceous fuel 16 and in order to reduce the calcium sulfate (CaSO4)28 to calcium sulfide (CaS) 24 in the reducing reactor 18, such as tothereby permit a continuous recycling thereof to be had. With furtherregard thereto, in accordance with the preferred mode of operation ofthe hot solids process 10 of the present invention that is depicted inFIG. 1 of the drawing, steam, and with the latter steam being denoted bythe arrow 30 in FIG. 1 of the drawing, is preferably also supplied as aninput to the reducing reactor 18.

Referring once again to FIG. 1 of the drawing, the burning of thecarbonaceous fuel 16 in the reducing reactor 18 is designed to be suchthat the predetermined output 12 is thus capable of being generated inthe reducing reactor 18, and with the carbon and the hydrogen containedin the carbonaceous fuel 16 being converted, in the course of suchburning of the carbonaceous fuel 16 to a product gas, such as, H2 orsyngas, in a suitable form such that such product gas, with the possibleaddition thereto of steam is capable of being made to function as thepredetermined output 12 from the hot solids process 10 of the presentinvention, in accordance with the preferred mode of operation thereof,which is designed to be suitable for use as an input to a petrochemicalprocess, such as, by way of exemplification and not limitation, thepredetermined process, which is schematically depicted at 14 in FIG. 1of the drawing. In addition, as is indicated in FIG. 1 of the drawing bythe arrow that is denoted therein by the reference numeral 32, thenitrogen (N2), which remains from the oxidation of the calcium sulfide(CaS) 24 that takes place in the oxidizing reactor 20, is designed to bemade to exit through an outlet (not shown in the interest of maintainingclarity of illustration in the drawing) with which the oxidizing reactor20 is designed to be suitably provided for this purpose.

For purposes of completing the description of the nature of theconstruction and of the mode of operation in accordance with the presentinvention of both the hot solids process 10 and the petrochemicalprocess 14, which are schematically depicted in FIG. 1 of the drawing,reference will once again be had herein to FIG. 1 of the drawing. Tothis end, in accordance with the mode of operation of the presentinvention the hot solids process 10 is suitably constructed so as to becapable of generating a predetermined output 12, such as, by way ofexemplification and not limitation, steam and H2 or syngas, that isdesigned to be suitable for use as an input to a petrochemical process,such as, for example, the petrochemical process, which is schematicallydepicted in FIG. 1 of the drawing.

With further reference to the petrochemical process, which isschematically depicted at 14 in FIG. 1 of the drawing, in accordancewith the conventional mode of operation of such petrochemical processes,crude, which is denoted by the arrow 34 in FIG. 1 of the drawing, isdesigned to be supplied as an input to the petrochemical process 14.Continuing with the discussion of the mode of operation thereof, thecrude 34 and the input 12, the latter being produced as an output fromthe hot solids process 10 of the present invention, are designed to besupplied as inputs to the petrochemical process 14 such that inaccordance with conventional practice the crude 34 and the input 12,which are supplied as inputs to the petrochemical process 14, aredesigned to be converted in known fashion through operation of thepetrochemical process 14 so as to thereby produce both a usable productoutput, the latter usable product output being denoted by the arrow 36in FIG. 1 of the drawing, that commonly consists of one or more of thefollowing: diesel fuel, gasoline, etc., and an otherwise normallyunusable product output 16 to which reference has been had hereinpreviously. With further regard thereto, in accordance with the presentinvention a portion of the otherwise normally unusable product output16, which preferably comprises, by way of exemplification and notlimitation, petcoke and/or oil residuals, from the petrochemical processthat is depicted at 14 in FIG. 1 of the drawing, is designed to beemployed in accordance with the present invention as an input to the hotsolids process 10 for purposes of effecting, in accordance with thepresent invention, the production within the hot solids process 10 ofthe predetermined output 12 that is designed to be suitable for purposesof being employed as the input 12 to the petrochemical process, which isschematically depicted at 14 in FIG. 1 of the drawing. The remainder ofthe otherwise normally unusable product output, such remainder beingdepicted in FIG. 1 of the drawing by the arrow that is denoted thereinby the reference numeral 17, which is produced from the petrochemicalprocess 14 that is schematically depicted in FIG. 1 of the drawing, issuitably designed such as to be capable of being discharged from thepetrochemical process 14 in any conventional manner, which is deemed tobe suitable for use for such a purpose.

While the embodiments of the present invention described hereinbeforeincluded a calcium oxide, the invention contemplates that the oxide mayinclude a metal oxide, for example, formed of iron such as FeO.

While a preferred embodiment of the present invention has been shown anddescribed in the instant application, it is to be understood thatvarious modifications and substitutions, some of which have been alludedto in the instant application, may be made thereto without departingfrom the spirit and scope of the present invention, as the presentinvention is set forth in the claims that are appended hereto.Accordingly, it is to be further understood that the present invention,as the present invention has been shown and described in the instantapplication, has been shown and described therein by way of illustrationonly, and not by way of limitation.

1. A hot solids process capable of generating a predetermined outputsuitable for use as an input to a petrochemical process comprising:providing a first reactor capable of operating as a reducing reactor;providing a second reactor capable of operating as an oxidizing reactor;supplying both a sulfur containing carbonaceous fuel and a source ofcalcium as inputs to the first reactor; supplying air as an input to thesecond reactor; effecting with the source of calcium the capture in thefirst reactor of the sulfur in the sulfur containing carbonaceous fuelso as to thereby produce CaS in the first reactor; effecting thedischarge as an output from the first reactor of the CaS produced in thefirst reactor; supplying as an input to the second reactor the CaSdischarged as an output from the first reactor; effecting the productionof CaSO4 in the second reactor from the CaS supplied as an input to thesecond reactor; effecting the discharge as an output from the secondreactor of the CaSO4 produced in the second reactor; supplying the CaSO4discharged as an output from the second reactor as an input to the firstreactor; effecting in the first reactor the generation of apredetermined output suitable for use as an input to a petrochemicalprocess by virtue of the utilization of the CaSO4 supplied to the firstreactor from the second reactor both as an oxygen source and as a heatsource; connecting in operative relation to the hot solids process apetrochemical process operable for purposes of producing a usableproduct output as well as an otherwise normally unusable product output;effecting the discharge as an output from the first reactor of thepredetermined output suitable for use as an input to a petrochemicalprocess produced in the first reactor; and supplying as an input to thepetrochemical process the predetermined output suitable for use as aninput to a petrochemical process that is discharged as an output fromthe first reactor.
 2. The hot solids process as claimed in claim 1further comprising selecting as the first reactor a circulating bedreactor capable of operating as a reducing reactor, and selecting as thesecond reactor a circulating bed reactor capable of operating as anoxidizing reactor.
 3. The hot solids process as claimed in claim 1further comprising selecting a portion of the otherwise normallyunusable product output from the petrochemical process for use as thesulfur containing carbonaceous fuel in the hot solids process.
 4. Thehot solids process as claimed in claim 3 further comprising supplying asan input to the first reactor of the hot solids process the portion ofthe otherwise normally unusable product output from the petrochemicalprocess selected for use as the sulfur containing carbonaceous fuel inthe hot solids process.
 5. The hot solids process as claimed in claim 4wherein the portion of the otherwise normally unusable product outputfrom the petrochemical process supplied as an input to the first reactorof the hot solids process for use as the sulfur containing carbonaceousfuel in the hot solids process comprises petcoke.
 6. The hot solidsprocess as claimed in claim 3 wherein the portion of the otherwisenormally unusable product output from the petrochemical process suppliedas an input to the first reactor of the hot solids process for use asthe sulfur containing carbonaceous fuel in the hot solids processcomprises residual oils.
 7. The hot solids process as claimed in claim 1further comprising selecting CaCO3 for use as the source of calciumsupplied as an input to the first reactor of the hot solids process. 8.The hot solids process as claimed in claim 1 wherein the predeterminedoutput suitable for use as an input to a petrochemical process that issupplied as an input to the petrochemical process from the first reactorof the hot solids process comprises H2.
 9. The hot solids process asclaimed in claim 8 wherein the predetermined output suitable for use asan input to a petrochemical process that is supplied as an input to thepetrochemical process from the first reactor of the hot solids processfurther comprises steam.
 10. The hot solids process as claimed in claim1 wherein the predetermined output suitable for use as an input to apetrochemical process that is supplied as an input to the petrochemicalprocess from the first reactor of the hot solids process comprisessyngas.
 11. The hot solids process as claimed in claim 10 wherein thepredetermined output suitable for use as an input to a petrochemicalprocess that is supplied as an input to the petrochemical process fromthe first reactor of the hot solids process further comprises steam. 12.A hot solids process capable of generating a predetermined outputsuitable for use as an input to a petrochemical process comprising:providing a first reactor capable of operating as a reducing reactor;providing a second reactor capable of operating as an oxidizing reactor;supplying both a sulfur containing carbonaceous fuel and an oxide asinputs to the first reactor; supplying air as an input to the secondreactor; effecting with the oxide the capture in the first reactor ofthe sulfur in the sulfur containing carbonaceous fuel; effecting theproduction of an oxide in the second reactor; effecting the discharge asan output from the second reactor of the oxide produced in the secondreactor; supplying the oxide discharged as an output from the secondreactor as an input to the first reactor; effecting in the first reactorthe generation of a predetermined output suitable for use as an input toa petrochemical process by virtue of the utilization of the oxidesupplied to the first reactor from the second reactor both as an oxygensource and as a heat source; connecting in operative relation to the hotsolids process a petrochemical process operable for purposes ofproducing a usable product output as well as an otherwise normallyunusable product output; effecting the discharge as an output from thefirst reactor of the predetermined output suitable for use as an inputto a petrochemical process produced in the first reactor; and supplyingas an input to the petrochemical process the predetermined outputsuitable for use as an input to a petrochemical process that isdischarged as an output from the first reactor.
 13. The hot solidsprocess as claimed in claim 12 wherein the oxide is one of a calciumoxide and metal oxide.